Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
  • B01J31/0277—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides comprising ionic liquids, as components in catalyst systems or catalysts per se, the ionic liquid compounds being used in the molten state at the respective reaction temperature
  • B01J31/0278—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides comprising ionic liquids, as components in catalyst systems or catalysts per se, the ionic liquid compounds being used in the molten state at the respective reaction temperature containing nitrogen as cationic centre
  • B01J31/0281—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides comprising ionic liquids, as components in catalyst systems or catalysts per se, the ionic liquid compounds being used in the molten state at the respective reaction temperature containing nitrogen as cationic centre the nitrogen being a ring member
  • B01J31/0284—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides comprising ionic liquids, as components in catalyst systems or catalysts per se, the ionic liquid compounds being used in the molten state at the respective reaction temperature containing nitrogen as cationic centre the nitrogen being a ring member of an aromatic ring, e.g. pyridinium
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
  • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
  • C07C2/56—Addition to acyclic hydrocarbons
  • C07C2/58—Catalytic processes
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
  • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
  • C07C2/56—Addition to acyclic hydrocarbons
  • C07C2/58—Catalytic processes
  • C07C2/60—Catalytic processes with halides
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G17/00—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge
  • C10G17/02—Refining of hydrocarbon oils in the absence of hydrogen, with acids, acid-forming compounds or acid-containing liquids, e.g. acid sludge with acids or acid-containing liquids, e.g. acid sludge
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
  • C10G29/20—Organic compounds not containing metal atoms
  • C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
  • C10L1/00—Liquid carbonaceous fuels
  • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
  • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
  • B01J2231/30—Addition reactions at carbon centres, i.e. to either C-C or C-X multiple bonds
  • B01J2231/32—Addition reactions to C=C or C-C triple bonds
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2527/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • C07C2527/06—Halogens; Compounds thereof
  • C07C2527/125—Compounds comprising a halogen and scandium, yttrium, aluminium, gallium, indium or thallium
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C2531/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • C07C2531/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
  • C10G2300/10—Feedstock materials
  • C10G2300/1088—Olefins
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
  • C10G2400/02—Gasoline
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
  • C10L2270/00—Specifically adapted fuels
  • C10L2270/02—Specifically adapted fuels for internal combustion engines
  • C10L2270/023—Specifically adapted fuels for internal combustion engines for gasoline engines

Definitions

• This application is directed to high quality alkylate gasoline and processes to produce high quality alkylate gasoline from olefin feeds comprising pentenes, while producing very low (or even no) isopentane from the olefin feed.
• Alkylate gasoline is a highly desirable blending component for motor gasoline with its high octane, low sulfur level and no aromatics.
• gasoline specifications have become tightened worldwide due to heightened environmental concerns, the demand for increased use of alkylate gasoline has been increasing steadily over the years.
• FCC fluid catalytic cracker
• the FCC units also produce a light gasoline fraction, containing substantial amount of C5 - Ce olefins, and due to the difficulties in performing alkylations with them, they are currently blended into the gasoline pool.
• This application provides a process to make an alkylate gasoline, comprising:
• a yield of the isopentane in the alkylate gasoline corresponds to less than 15 mol% of C5 olefins in the olefin feed and wherein the alkylate gasoline has a final boiling point from 370 °F (187.8 degree Celsius) to 400 °F (204.4 degree Celsius) and a RON of 85 or greater.
• This application also provides an alkylation process comprising:
• the olefin feed comprises at least 8 wt% pentenes and less than 60 wt% isopentane
• a yield of the isopentane in the alkylate gasoline corresponds to less than 15 mol% of C5 olefins in the olefin feed
• the alkylate gasoline has a final boiling point from 370 °F (187.8 degree Celsius) to 400 °F (204.4 degree Celsius) and a RON of 85 or higher;
• an n-pentane product yield relative to a total olefin content in the olefin feed is from zero to less than 0.2 mol/mol.
• this application provides an alkylate gasoline, comprising less than 0.1 wt% olefins, less than 0.1 wt% aromatics, less than 1.8 wt% C12+ hydrocarbons, and greater than 60 wt% Cs hydrocarbons and C9 hydrocarbons, wherein an amount of a trimethylpentane in the Cs hydrocarbons is from 70 to 80 wt% and a second amount of a trimethylhexane in the C9 hydrocarbons is from 80 to 90 wt%.
• the present invention may suitably comprise, consist of, or consist essentially of, the elements in the claims, as described herein.
• Olefin refers to a class of unsaturated aliphatic hydrocarbons having one or more double bonds
• Pentenes are alkenes with the chemical formula C5H10. Each pentene molecule contains one double bond within its molecular structure. There are a total of six different pentene compounds, differing from each other by whether the carbon atoms are attached linearly or in a branched structure, and whether the double bond has a cis- or trans- form.
• Isoparaffin refers to a branched isomer of a straight-chain paraffin molecule.
• Alkylate gasoline refers to hydrocarbons that are composed of a mixture of high- octane, branched-chain paraffinic hydrocarbons (e.g., isoheptane and isooctane). Alkylate gasoline is a premium gasoline blending stock because it has exceptional antiknock properties and is clean burning.
• FCC Fluid catalytic cracker
• Periodic Table refers to the version of the IUPAC Periodic Table of the Elements dated June 22, 2007, and the numbering scheme for the Periodic Table Groups is as described in Chemical And Engineering News, 63(5), 27 (1985).
• Acidic ionic liquid refers to materials consisting entirely of ions, that can donate a proton or accept an electron pair in reactions, and that are liquid below 100°C.
• an acidic ionic liquid alkylation catalyst is effective in alkylating a Cs olefin feed with isobutane to make excellent quality alkylate gasoline.
• Our processes can operate in a wide range of feed variation with both excellent operability and product selectivity.
• our process with an acidic ionic liquid alkylation catalyst can selectively convert the C5 olefins to alkylate gasoline with a minor (or no) incremental production of isopentane.
• our processes are able to convert both isopentane and C5 olefins in the feed to alkylate gasoline and thus, effectively lower the isopentane content in the alkylate gasoline product.
• Alkylation of C5 olefins (pentenes or amylenes) with isoparaffins comprising isobutane would provide many benefits to a refinery.
• a refinery would be able to increase the alkylate gasoline production volume by alkylating the C5 olefins with isobutane and the alkylate gasoline has a significantly higher value than the isobutane and the mixed pentene starting materials.
• RVP alkylate gasoline by converting the high RVP (Reid Vapor Pressure) and olefinic pentenes from a Fluid Catalytic Cracker (FCC) gasoline to generate low RVP alkylate gasoline by the processes of our invention, the overall gasoline pool RVP and olefin content are significantly reduced.
• FCC Fluid Catalytic Cracker
• the olefin feed that is useful in the processes herein comprise at least 8 wt% of pentenes and less than 60 wt% isopentane. In one embodiment, the olefin feed comprises greater than 20 wt% of pentenes. In one embodiment, the olefin feed comprises from at least 8 wt% to 100 wt% pentenes.
• the amount of the pentenes in the olefin feed can range broadly, for example the amount of the pentenes in the olefin feed can be from 10 to 100 mol%, from 10 to 99.9 mol%, or 35 to 100 mol% of a total olefins in the olefin feed.
• the olefin feed additionally comprises a butene, such as from 1 to 80 wt% butene.
• the olefin feed comprises C3, C 4 , and C5 olefins.
• the olefin feed can come from any source, not just from a refinery. Examples of suitable olefin feeds include hydrocarbons comprising pentenes which could come, for example, from FCC, from a coker unit, naphtha cracking, gas-to-liquid (GTL) processes, or derived via dehydrogenation of pentane, such as from natural gas liquid dehydrogenation or bio-material dehydrogenation.
• the feeds may come directly from different sources, or can be blended.
• the olefin feed is from a FCC unit in a refinery.
• the processes may additionally comprise isolating a Cs olefin stream from a FCC unit to provide the olefin feed and the alkylating converts the Cs olefin stream to the alkylate gasoline without needing to increase a throughput from the FCC unit.
• the olefin feed comprises 1-pentene, such as from greater than 2 wt% to 10 wt% 1 -pentene.
• the olefin feed may comprise varying levels of w-pentane.
• the olefin feed comprises from zero to 10 wt% w-pentane, such as 4 wt% or less, or from 0.1 wt% to 8 wt% ft-pentane.
• the olefin feed comprises greater than 5 wt% isopentane, such as from greater than 12.7 wt% to 55 wt% of the isopentane. In one embodiment, the olefin feed comprises greater than 12.7 wt% of the isopentane and the alkylating lowers a content of the isopentane in the alkylate gasoline.
• the processes may comprise selectively hydrogenating a refinery olefin stream to make the olefin feed.
• the selectively hydrogenating can reduce the dienes in the olefin feed.
• the olefin feed can comprise less than 1 wt% dienes, or from zero to 0.5 wt% dienes. Reducing the level of dienes and cyclopentene in the olefin feed can reduce the rate of conjunct polymer formation during the alkylating and/or improve the alkylate gasoline product quality, e.g., by reducing formation of gum or heavy hydrocarbons with high boiling point.
• the conditions for selectively hydrogenating are selected to be mild, and the mild conditions remove only a portion of the dienes.
• the conditions for selectively hydrogenating are chosen to also perform olefin isomerization, and the olefin isomerization can be limited to shifting of double bonds in molecules in the olefin feed, such as converting 1-pentene to 2-pentene or converting methyl-l-butenes to methyl-2-butenes. Conversion of 1-pentene to 2-pentene, thereby increasing the relative amount of 2-pentene in the olefin feed, can increase the RON and MON of the alkylate gasoline produced via alkylation with an ionic liquid catalyst.
• the processes may additionally comprise hydroisomerizing a refinery olefin stream to make an olefin feed that has a reduced amount of 1-butene and an increased amount of 2-butene.
• Increasing the amount of 2-butene in the olefin feed can increase the RON and/or a MON of the alkylate gasoline.
• the processes may comprise selectively hydrogenating the olefin feed to increase the RON and/or a MON of the alkylate gasoline by at least about 0.5.
• the RON is increased by 0.5 to 4.0.
• the alkylating can convert essentially all of the olefins in the olefin feed. In one embodiment, the alkylating converts greater than 98 wt%, or even 100 wt%, of the olefins in the olefin feed.
• the alkylate gasoline made by the processes disclosed herein has one or more of a high Research Octane Number (RON), a high Motor Octane Number (MON), a low final boiling point, and low Reid Vapor Pressure (RVP).
• the alkylate gasoline produced by the processes of this invention can have one or more desired properties, including a low final boiling point, a high RON, high MON, low RVP, low aromatics, low olefins, and low sulfur.
• the alkylate gasoline has a final boiling point from 370 °F (187.8 degree Celsius) to 400 °F (204.4 degree Celsius).
• Research Octane Number (RON) is determined using ASTM D2699-15 (REV A), Standard Test Method for Research Octane Number of Spark-Ignition Engine Fuel.
• RON can be calculated from gas chromatography boiling range distribution data.
• the RON (GC) calculation is described in the publication, Anderson, P. C, Sharkey, J. M., and Walsh, R. P., "Journal Institute of Petroleum", 58 (560), 83 (1972).
• Another measure of the octane number of a fuel is the Motor Octane Number (MON).
• MON correlates with commercial automotive spark-ignition engine antiknock performance under severe conditions of operation. MON can be determined by ASTM D2700-16.
• the alkylate gasoline has a high RON, such as 85 or higher, from 90.0 or higher, from 85.0 to 96.0, or from 90.0 to 94.5.
• the alkylate gasoline contains from zero to less than 0.1 wt% aromatics, from zero to less than 0.1 wt% olefins, and can also have low sulfur.
• the alkylate gasoline has an amount of a trimethylpentane in C8 hydrocarbons in the alkylate gasoline that is greater than 50 wt%, such as from 70 to 95 wt%.
• the alkylate gasoline has an amount of trimethylhexane in C9 hydrocarbons in the alkylate gasoline that is greater than 70 wt%, such as from 85 to 95 wt%.
• the alkylate gasoline comprises a C5+ alkylate fraction having a RVP less than 7 psi, such as from 2.3 to 6.0 psi, or from 2.0 to 5.5 psi. In one embodiment the RVP is less than 4.0 psi. RVP can be determined by ASTM D323-15a, "Standard Test Method for Vapor Pressure of Petroleum Products (Reid Method)".
• the alkylate gasoline has a C5+ average density greater than
• the alkylate gasoline comprises from zero to less than 0.1 wt% olefins, from zero to less than 0.1 wt% aromatics, from zero to less than 1.8 wt% C12+ hydrocarbons, and greater than 60 wt% combined Cs and C9 hydrocarbons.
• this alkylate gasoline can comprise a high level of trimethylalkanes, which impart a high RON to the alkylate gasoline.
• the alkylate gasoline can comprise an amount of a trimethylpentane in the Cs hydrocarbons greater than 50 wt%, such as from 70 to 95 wt%, and a second amount of a trimethylhexane in the C9 hydrocarbons greater than 70 wt%, such as from 85 to 95 wt%.
• the alkylate gasoline comprises from 0.1 to less than 1 wt% C12+ hydrocarbons.
• the alkylate gasoline comprises greater than 60 wt% Cs hydrocarbons and C9 hydrocarbons, such as from 61 to 90 wt% or 65 to 80 wt%. In one embodiment, the alkylate gasoline comprises greater than 10 wt% C9 hydrocarbons, such as from 13 to 42 wt%. In one embodiment, the alkylate gasoline comprises greater than 20 wt% C8 hydrocarbons, such as from 25 to 65 wt% Cs hydrocarbons.
• a C5 olefin stream from a FCC unit can be easily isolated and then this C5 olefin stream provides an attractive alternative source of olefins that can be converted to additional amounts of high quality, clean, alkylate gasoline without increasing the FCC unit throughput.
• the process is an effective alkylation process for a mixed C4/C5 olefin feed with isobutane using an acidic ionic liquid alkylation catalyst where the process selectively converts C5 olefins to alkylate gasoline with a minor incremental production of isopentane.
• our process is able to convert both isopentane and C5 olefins in the olefin feed to alkylate gasoline and also effectively lower the isopentane content in the alkylate gasoline product.
• the processes comprise alkylating the olefin feed with the isoparaffin feed using an acidic ionic liquid alkylation catalyst under alkylation conditions.
• the alkylating can be done at an alkylation temperature greater than -20 °C, such as from -15 °C to 100 °C, or from -10 °C to 50 °C.
• the alkylation conditions may include one or more of a catalyst volume in an alkylation reactor of 2 vol % to 50 vol %, an alkylation temperature of -10° C. to 100° C, an alkylating pressure of 300 kPa to 2500 kPa, an isoparaffin to olefin molar ratio of 2 to 16 and a residence time of 30 seconds to 1 hour.
• the acidic ionic liquid alkylation catalyst does not have a high H-transfer tendency, unlike the conventional HF alkylation catalyst and to a lesser extent than the H2SO4 alkylation catalyst.
• the acidic ionic liquid alkylation catalyst can preferably make the primary alkylation product of isobutane with C5 olefins that is predominately trimethylhexane.
• the acidic ionic liquid alkylation catalyst is uniquely able to convert isopentane in the olefin feed when the isopentane concentration is above a threshold value, somewhere between 12.7 to 29.8 wt% isopentane in the olefin feed or 1-3 wt% isopentane in the combined feed (isobutane and olefin feed).
• the acidic ionic liquid alkylation catalyst conducts simultaneous conversion of the isobutane and the isopentane into the alkylate gasoline during the alkylating. In one embodiment, the acidic ionic liquid alkylation catalyst conducts simultaneous conversion of isobutane and isopentane into high quality alkylate gasoline products. The simultaneous conversion of isobutane and isopentane appears to be unique, and this may allow co-processing of isopentane and isobutane in the alkylation reactor, which was not possible with earlier conventional alkylation catalysts. Acidic Ionic Liquid
• the acidic ionic liquid alkylation catalyst is a composite ionic liquid alkylation catalyst, wherein the cations come from a hydrohalide of an alkyl-containing amine or pyridine, and the anions are composite coordinate anions coming from two or more metal compounds.
• the most common acidic ionic liquids are those prepared from organic-based cations and inorganic or organic anions.
• the acidic ionic liquid alkylation catalyst is composed of at least two components which form a complex.
• the acidic ionic liquid alkylation catalyst comprises a first component and a second component.
• the first component of the acidic ionic liquid alkylation catalyst will typically comprise a Lewis acid compound selected from components such as Lewis acid compounds of Group 13 metals, including aluminum halides, alkyl aluminum dihalides, gallium halide, and alkyl gallium halide (see the Periodic Table, which defines the elements that are Group 13 metals). Other Lewis acid compounds besides those of Group 13 metals may also be used.
• the first component is aluminum halide or alkyl aluminum dihalide.
• aluminum trichloride AlCh
• AlCh aluminum trichloride
• the alkyl aluminum dihalides that can be used can have the general formula AI2X4R2, where each X represents a halogen, selected for example from chlorine and bromine, each R represents a hydrocarbyl group comprising 1 to 12 atoms of carbon, aromatic or aliphatic, with a branched or a linear chain.
• alkyl aluminum dihalides include dichloromethylaluminum, dibromomethylaluminum,
• dichloroisobutylaluminum either used separately or combined.
• the second component making up the acidic ionic liquid can be an organic salt or mixture of salts. These salts may be characterized by the general formula Q+A-, wherein Q+ is an ammonium, phosphonium, boronium, oxonium, iodonium, or sulfonium cation and A- is a negatively charged ion such as Cl ⁇ Br, C10 4 , NO3 ⁇ BF 4 , BC , PFe , SbFe " AIC " AI2CI7 - AbCho " GaCLT, Ga 2 Cl 7 ⁇ GasClio " AsFe " TaFe , CuCk “ FeCh “ AlBr , AkBrv , AbBno " , SO3CF3 , and 3-sulfurtrioxyphenyl.
• the second component is selected from those having quaternary ammonium halides containing one or more alkyl moieties having from about 1 to about 9 carbon atoms, such as, for example
• methyltributylammonium 1 -butyl pyridinium, or alkyl substituted imidazolium halides, such as for example, l-ethyl-3-methyl-imidazolium chloride.
• the acidic ionic liquid comprises a monovalent cation selected from the group consisting of a pyridinium ion, an imidazolium ion, a pyridazinium ion, a pyrazolium ion, an imidazolinium ion, a imidazolidinium ion, an ammonium ion, a phosphonium ion, and mixtures thereof.
• Examples of possible cations (Q+) include a butylethylimidazolium cation [ mecanic], a butylmethylimidazolium cation [bmim],
• tetraheptylammonium cation [hphphphp-N], a tetrahexylammonium cation [hxhxhxhx-N], a methylammonium cation [m-N], a dimethylammonium cation [mm-N], a
• the second component is selected from those having quaternary phosphonium halides containing one or more alkyl moieties having from 1 to 12 carbon atoms, such as, for example, trialkyphosphonium hydrochloride, tetraalkylphosphonium chlorides, and methyltrialkyphosphonium halide.
• the acidic ionic liquid comprises an unsubstituted or partly alkylated ammonium ion.
• the acidic ionic liquid is chloroaluminate or a bromoaluminate.
• the acidic ionic liquid is a quaternary ammonium chloroaluminate ionic liquid having the general formula RR' R" N H + AI2CI7 " , wherein R, R', and R" are alkyl groups containing 1 to 12 carbons.
• quatemary ammonium chloroaluminate ionic liquids are an N-alkyl-pyridinium chloroaluminate, an N-alkyl-alkylpyridinium
• chloroaluminate a pyridinium hydrogen chloroaluminate, an alkyl pyridinium hydrogen chloroaluminate, a di alkyl- imidazolium chloroaluminate, a tetra-alkyl-ammonium chloroaluminate, a tri-alkyl-ammonium hydrogen chloroaluminate, or a mixture thereof.
• the presence of the first component should give the acidic ionic liquid a Lewis or
• Franklin acidic character Generally, the greater the mole ratio of the first component to the second component, the greater is the acidity of the acidic ionic liquid.
• chloroaluminate ionic liquid is shown below:
• the acidic ionic liquid utilizes a co-catalyst to provide enhanced or improved alkylation activity.
• co-catalysts include alkyl halide or hydrogen halide.
• a co-catalyst can comprise, for example, anhydrous HCl or organic chloride (see, e.g., U.S. Pat. Nos. 7,495,144 to Elomari, and 7,531,707 to Harris et al).
• organic chloride is used as the co-catalyst with the acidic ionic liquid
• HCl may be formed in situ in the apparatus either during the alkylating or during post-processing of the output of the alkylating.
• the alkylating with the acidic ionic liquid is conducted in the presence of a hydrogen halide, e.g., HCl.
• the acidic ionic liquid alkylation catalyst additionally comprises a Bronsted acid.
• the acidic ionic liquid alkylation catalyst comprises an ionic liquid catalyst and a Bronsted acid.
• the Bronsted acid acts as a promoter or co-catalyst. Examples of Bronsted acids are sulfuric acid, HCl, HBr, HF, phosphoric acid, HI, etc. Other strong acids that are proton donors can also be suitable Bronsted acids.
• the Bronsted acid is produced internally within the process by the conversion of an alkyl halide into the corresponding hydrogen halide.
• the Bronsted acid is formed by a reaction of a Lewis acid component of an ionic liquid, such as chloroaluminate ions for instance reacting with a weakly acidic proton donor such as an alcohol or water to form HCl.
• a Lewis acid component of an ionic liquid such as chloroaluminate ions
• a weakly acidic proton donor such as an alcohol or water to form HCl.
• the alkyl halides that may be used include alkyl bromides, alkyl chlorides and alkyl iodides.
• alkyl halides include but are not limited to isopentyl halides, isobutyl halides, t- butyl halides, n-butyl halides, propyl halides, and ethyl halides.
• Alkyl chloride versions of these alkyl halides can be preferable when chloroaluminate ionic liquids are used.
• Other alkyl chlorides or alkyl halides having from 1 to 8 carbon atoms can be also used.
• the alkyl halides may be used alone or in combination.
• the alkyl halide or hydrogen halide co-catalysts are used in catalytic amounts.
• the amounts of the alkyl halides or hydrogen halide should be kept at low concentrations and not exceed the molar concentration of the AlCh in the acidic ionic liquid.
• the amounts of the alkyl halides or hydrogen halide used may range from 0.05 mol %-100 mol %, or 0.05 mol% - 10 mol%, of the Lewis acid AlCh in the acidic ionic liquid in order to keep the acidity of the acidic ionic liquid alkylation catalyst at the desired performing capacity.
• the acidic ionic liquid alkylation catalyst comprises an ionic liquid catalyst and a Bronsted acid.
• the Bronsted acid acts as a promoter or co-catalyst. Examples of Bronsted acids are sulfuric acid, HC1, HBr, HF, phosphoric acid, HI, etc. Other strong acids that are proton donors can also be suitable Bronsted acids.
• the Bronsted acid is produced internally within the process by the conversion of an alkyl halide into the corresponding hydrogen halide.
• the process can additionally comprise recycling an excess of the isoparaffin feed to the alkylating.
• the process can include distilling out an excess isoparaffin after the alkylating and then recycling the excess isoparaffin to the alkylating.
• the isobutane feeds used in this example were either refinery isobutane feed consisting of 85 wt% isobutane and 15 wt% n-butane, or 100 wt% pure chemical grade isobutane.
• the isobutane streams were thoroughly dried to less than 1 wppm water by passing the isobutane feeds through a fixed bed containing a molecular sieve adsorbent.
• olefin feeds used in this example were refinery olefin streams from a Fluid Catalytic Cracker (FCC) containing varying amounts of Cs olefins.
• the olefin feeds all had 1 wt% or less of C3 olefins, and no ethylene.
• These olefin feeds were also thoroughly dried to less than 1 wppm water by passing the olefin feeds through a fixed bed containing a molecular sieve adsorbent.
• the water contents in the dried isobutane and olefin feeds were measured using a GE Panametrics on-line moisture analyzer with an aluminum oxide moisture sensor probe.
• Feed #3 was analyzed for precise cyclopentene and diene content measurements, Feed #2, Feed #4 and Feed #5 are expected to have similar amounts of cyclopentene and dienes.
• Feed # 1 was a typical refinery feed for a C4 olefin alkylation plant and is a comparative example.
• the C5 olefin content was low, 1.5 wt%, and the amount of C5 olefin relative to the total olefins was only 2.2 mol%.
• the feed # 1 contained only 3.2 wt% isopentane.
• olefin feeds contained from 12.7 to 48.5 wt% isopentane. These olefin feeds contained from 0.7 to 3.7 wt% n-pentane.
• the olefin Feeds #2 through #5 were selectively hydrogenated at mild conditions to reduce their diene contents. These olefin feeds still contained about 300-700 ppm of butadiene, 1 100 ppm of isoprene (2-methyl-l,3-butadiene), 400 ppm of trans-l ,3-pentadiene and 500 ppm of cyclo-pentadiene.
• the selective hydrogenation of Feed # 1 was more extensive, and nearly complete removal of butadiene was observed (less than the detection limit of 100 ppm by GC). Examples 3 through 7; Alkylation Conditions and Alkylate Gasoline Products
• the reactor effluent was separated with a coalescing separator into a hydrocarbon phase and an ionic liquid alkylation catalyst phase.
• the hydrocarbon phase was further separated with three distillation columns into multiple streams, including: a gas stream containing a C3 " fraction, an nC4 stream, an 1C4 stream, and an alkylate gasoline stream.
• the separated ionic liquid alkylation catalyst was sent to a regeneration reactor for reduction of the conjunct polymer level in the acidic ionic liquid alkylation catalyst.
• the conjunct polymer level in the acidic ionic liquid alkylation catalyst was maintained at 3-6 wt%.
• the amount of conjunct polymer in the acidic ionic liquid alkylation catalyst was determined using an FT-IR quantitation method described in US patent No. US9290702B2.
• Example 3 with Feed #1
• the base case showed the typical yield and product properties for alkylation of C4 olefins.
• Alkylation performance of Example 3 was compared with the other olefin feeds with higher C5 (and varied) olefin feed compositions. Increases of the C5 olefin content in the olefin feed from 14.2 mol% to 75 mol% (Feed #2 through Feed #5), did not affect the unit operation in any negative ways. In all cases, the olefin conversions were maintained at 100% and the residual olefin contents in the alkylate gasoline products were less than 0.1 wt%.
• the alkylate gasoline products had RONs in the range of 94.5 to 90 and MONs in the range of 92.3 to 89. These octane numbers were decreased slightly due to the increased Css (that came with the feed), a reduction of the Cs hydrocarbons in the alkylate gasoline products, and an increase of the C9 hydrocarbons in the alkylate gasoline products.
• the C9 hydrocarbon fractions in the alkylate gasoline products were rich in trimethylhexanes (from 75.7 to 85.9 wt%), which have a relatively low RON of 90.
• the Cs hydrocarbon fractions in the alkylate gasoline products were also rich in trimethylpentanes, which have a high RON of 100.
• the isopentane and w-pentane that was present in the olefin feeds was incorporated into the alkylate gasoline products and made the analysis of the alkylate gasoline products more complicated.
• the alkylation process we employed can make isopentane or «-pentane, and the amount of the synthesized isopentane or w-pentane needed to be differentiated from the corresponding components that came with the olefin feeds.
• the yields of the synthesized hydrocarbon products by the alkylation process are called herein as “true” yields.
• material balance calculations around the alkylation process unit were conducted. Using the data with >97% material balance closures, the isopentane and n- pentane amounts supplied by the olefin feeds were subtracted from the apparent alkylate gasoline product amounts, and the "true” yields were thus estimated.
• the "true” yield results are summarized in Table 4. Table 4
• the yield of isopentane from C5 olefins for the Example 4 was estimated to be about 9 wt% or 14 mol%..

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